CN100509133C

CN100509133C - Method of filling solid catalyst

Info

Publication number: CN100509133C
Application number: CNB2004800006055A
Authority: CN
Inventors: 田泽和治; 勅使河原力; 齐藤辉雄
Original assignee: Mitsubishi Kasei Corp
Current assignee: Mitsubishi Chemical Corp; Mitsubishi Rayon Co Ltd
Priority date: 2004-01-22
Filing date: 2004-09-29
Publication date: 2009-07-08
Anticipated expiration: 2024-09-29
Also published as: US20050161373A1; CN1697685A; US7147011B2; JP2005205320A; EP1726358A4; EP1726358A1; WO2005070531A1; ZA200500202B

Abstract

A method for packing a solid catalyst is provided, whereby the pressure loss of a reaction tube packed with the catalyst can be reduced. The method is characterized in that prior to packing a solid catalyst in a reactor, the solid catalyst is sieved to remove a cracked catalyst. For example, sieving is carried out against a solid catalyst of a columnar or cylindrical shape having an outer diameter A being larger than the length B in the axial direction by using a sieve having a sieve mesh with a width C satisfying the condition of A>C>B and a length being at least the width, or against a solid catalyst of a columnar or cylindrical shape with an outer diameter A being from 1 to 0.5 time the length B in the axial direction by using a sieve having a sieve mesh with a width C satisfying the condition of A>C>0.5B and a length being at least the width.

Description

The method of filling solid catalyst

Technical field

The present invention relates to the method for filling solid catalyst in reactor, particularly wherein in fixed bed reactors, screen the method for solid catalyst before the filling.

Background technology

For filling mould controlling catalyst or carried catalyst in fixed bed reactors, the packing method that generally adopts catalyst wherein to fall from reactor top.In this method, may when fall, be ground by physical impact or be cracked by catalyst.This trend does not have under the situation of high mechanical properties obvious especially at molded catalyst or carried catalyst.Following can be that catalyst is pulverized or cracked method when being suppressed at filling.

By dropping under the situation of loading catalyst the reactor from reactor top, known method is to provide to have the band (string) (patent documentation 1) that does not hinder the shape and size that catalyst falls basically in reactor.In addition, when when being installed in the reaction tube the reactor filling solid catalyst from reaction tube top whereabouts catalyst, known method is a filling liquid in reaction tube at first wherein, and filling solid catalyst is removed liquid (patent documentation 2) afterwards from reaction tube then.In addition, as another method, known method is before the reaction tube that enters reactor by the whereabouts comes filling solid catalyst, loads dry ice in reaction tube, and loading catalyst is removed dry ice (patent documentation 3) by gasification then then.

Patent documentation 1:JP-A-5-31351

Patent documentation 2:JP-A-9-141084

Patent documentation 3:JP-A-10-277381

Summary of the invention

The problem to be solved in the present invention

The molded catalyst or the carried catalyst that do not have high mechanical properties not only enter pulverizing or cracked easily in the reactor process in filling, and before filling, broken by physical impact, rousing after the production in (drum) when storing, the catalyst of drum bottom breaks easily.This catalyst that breaks has the mechanical strength that further weakens, thereby easier pulverizing in filling.In addition, the filling gap of catalyst is full of probably breaks and the catalyst of refinement, thereby not only the loading density of catalyst increases, and the pressure loss of reaction tube will increase.

Therefore, when will be in reaction tube during loading catalyst, must remove the catalyst that breaks that comprises in the catalyst.In this case, if removing of the catalyst that breaks is inadequate, compare with the situation of filling crack-free normal catalytic agent in reaction tube, the above-mentioned loading density and the pressure loss will increase, thereby reaction can not be carried out under the predetermined running state.

Above-mentioned patent documentation 1 to 3, the method of loading catalyst to avoid breaking in reaction tube only disclosed, but do not have the method open or catalyst that had broken is effectively removed in proposition before filling, and can be by removing the catalyst that breaks to reduce the method for the reaction tube pressure loss.Therefore, even patent documentation 1 does not take place to pulverize during disclosed loading catalyst in 3 or be cracked, if sneaked into the catalyst that breaks before filling, then this catalyst that breaks will load as it is and enter reaction tube, therefore can not address the above problem.

An object of the present invention is to provide a kind of when filling solid catalyst when for example molded catalyst or carried catalyst enter fixed bed reactors, the method for before filling, removing this catalyst that breaks that causes the reaction tube pressure loss effectively.

The mode of dealing with problems

Research and solve the result of the problems referred to above as many-side, realized the present invention based on following discovery: can remove the catalyst that breaks to reduce the pressure loss of reactor by screening, if use in addition to have specified sieve purpose screen cloth and screen, can remove the catalyst that breaks effectively.That is, the invention provides the method for following filling solid catalyst.

1. the method for a filling solid catalyst is characterized as in reactor and before the filling solid catalyst, screens solid catalyst to remove the catalyst that breaks.

2. the method for above-mentioned 1 filling solid catalyst, wherein have the screen cloth of width as the sieve mesh of C by using, outer diameter A is screened the sieve mesh A that satisfies condition greater than the cylindrical of axial length B or cylindrical solids catalyst〉C〉B, the length of sieve mesh is at least width.

3. the method for above-mentioned 1 filling solid catalyst wherein has the screen cloth of diameter as the circular sieve mesh of C by using, to outer diameter A than axial length B

Doubly big cylindrical or cylindrical solids catalyst screens, the sieve mesh A that satisfies condition〉C〉B.

4. the method for above-mentioned 1 filling solid catalyst, wherein have the screen cloth of width as the sieve mesh of C by using, to outer diameter A is that 1 to 0.5 times cylindrical or cylindrical solids catalyst of axial length B screens, the sieve mesh A that satisfies condition〉C〉0.5B, the length of sieve mesh is at least width.

5. according to the method for above-mentioned 2 to 4 any one filling solid catalysts, wherein the ratio of C and A is at least 90%.

6. the method for above-mentioned 1 filling solid catalyst wherein uses width to be the spherical solid catalyst of the screen cloth of the sieve mesh of E screening external diameter as D, the sieve mesh D that satisfies condition〉E〉0.5D, the length of sieve mesh is greater than D.

Effect of the present invention

According to the present invention, in the reaction tube of fixed bed reactors before the filling with having specified sieve purpose mesh screen modeling controlling catalyst or carried catalyst, thereby can remove the catalyst that breaks effectively.Thereby can reduce the pressure loss of the reaction tube of loading catalyst, and can provide excellent effect at stable operation reactor under the rated condition.

Description of drawings

Fig. 1 is the perspective view of the cylindric catalyst of the present invention.

Fig. 2 is the perspective view of cylinder shape catalyst of the present invention.

Fig. 3 is the diagrammatic view that the cylinder shape catalyst flat surfaces breaks.

Fig. 4 is the diagrammatic view that breaks in the cylinder shape catalyst side.

Fig. 5 is a rectangular mesh screen purpose partial view.

The symbol implication

1: catalyst

2: opening portion

3: the part of breaking

4: flat surfaces (flat surface)

The specific embodiment

Solid catalyst shape of the present invention can be used for and sphere, cylindrical and cylindrical shape can be selected from.The molded catalyst that for example common pelleter, extruder or the rotary drum granulator (tumbling granulator) of known employing forms.When adopting carried catalyst, the type of carrier is not particularly limited, and for example can use common carrier for example silica, aluminium oxide, silica/alumina, magnesia or titanium oxide.The shape of carried catalyst can also be selected from the sphere of similar above-mentioned molded catalyst, cylindrical and cylindrical shape.Solid catalyst comprises this carried catalyst among the present invention, is called for short term ＂ catalyst ＂ and is meant solid catalyst.

As mentioned above, solid catalyst may be broken by physical impact during the Catalyst Production step, or during the catalyst stores or migration of producing in drum etc., catalyst may be cracked under loading in the drum bottom.Among the present invention, be called by this cracking of normal catalytic agent or the pulverizing (comprising efflorescence) of breaking and break, this catalyst of obtaining of breaking is commonly called the ＂ catalyst ＂ that breaks.When the intensity at catalyst of breaking of this catalyst is fragile more, easy more generation, but the intensity of catalyst changes with the shape or the size of catalyst, even identical materials.

The mode of breaking in addition, changes with the shape of catalyst.Usually, cylindrical shape or cylinder shape catalyst break than spheric catalyst is easier, and cylindrical shape or cylinder shape catalyst flatly or elongated break easily along with becoming.In addition, bigger smaller easier breaking.

To describe this of catalyst now in detail breaks.Fig. 1 has shown that the heart therein has the cylinder catalyst 1 of opening 2, and Fig. 2 shown cylinder shape catalyst 1.In this cylindrical shape or cylinder shape catalyst 1, A represents the external diameter of catalyst 1, and B represents axial length (highly).For this catalyst 1, if A becomes greater than B, catalyst 1 becomes flat, otherwise, if it is B becomes greater than A, axially elongated.When with external force or concussion fracture cylindrical shape or cylinder shape catalyst 1, long size is easier to be stressed, and therefore, the direction of breaking (failure mode) depends on that usually catalyst 1 is flat or elongated.Direction is axial (length direction) or the direction (laterally) of vertical axial of catalyst 1, and the breaking of catalyst 1 can be divided into breaking at flat surface usually promptly axially breaks and break and promptly break in direction perpendicular to axial direction in the side.Cylinder shape catalyst and cylinder catalyst are basic identical in the breaking of catalyst 1.Therefore, hereinafter, the description of circle of reference cylindricality catalyst is broken.

As shown in Figure 3, from flat surfaces 4 beginning of catalyst 1 flat surface gash fracture at axial cylindrical shape catalyst 1.Position on the flat surfaces 4 that begins to break can not determine to it depends on intensity of force or force way, but catalyst 1 because of the crack in the flat surfaces along axially being separated.For example, as shown in Figure 3, if cylinder shape catalyst 1 breaks on the right flank on circular, flat surface 4, it is divided into major part (solid line part) and less than the part 3 of breaking (two empty chain line) of major part.Be formed on the crack in the flat surfaces probably therein on the flat catalyst of outer diameter A greater than axial length B.May only break in theory (cracked chipped off) at axial component, but in fact because it is a flat pattern, most of for axially breaking along whole as shown in Figure 3, be few axially having the cracked catalyst of part.Therefore, when the catalyst that screening the present invention is axially broken, the catalyst shape of the catalyst that axial whole length is broken is a target, is not target axially having the cracked catalyst of part.Yet, axially have the cracked part target that yes will remove of the cracked catalyst of part.

On the other hand, breaking of catalyst side is to break perpendicular to catalyst 1 axial direction, and as shown in Figure 4, it is considered to make breaking that axial length shortens.As long as it is perpendicular to axial the breaking of catalyst, it can be can not orthogonal vertical breaking in axial inclination.Only in the situation of direction partial rupture perpendicular to axial direction (cracked), will remove with the identical cracked part of breaking in the above-mentioned flat surfaces, not to be shorter than axial major part be not the target that will remove but all the other have length.Break and be subject to often take place in the elongated catalyst of A＜B of external force influence for side wherein in this side.

Although do not show in the accompanying drawing, breaking of spheric catalyst is considered to separating of spheroid usually.Yet the catalyst with the cracked spheroid of suitable major part also is the object that will remove.

Now, will method that use screen cloth to remove the catalyst that breaks be described.＂ screen cloth ＂ here be install or be equipped with have the base material of specifying sieve mesh, as the general term of instrument, instrument or the device of the net of important document or plate, ＂ screening ＂ is meant the unit operations that uses this screen cloth will be not to be separated by the material of sieve mesh and material by sieve mesh.Among the present invention, the device of removing the catalyst that breaks is not particularly limited, as long as it is the screen cloth with this screening function.

Be generally used for screening the screen cloth that the screen cloth of operation normally has sieve meshes such as square, rectangle, rhombus, hexagon or circle.In this case, in the relation of sieve mesh and the catalyst granules that will screen, according to the distance between the parallel tangents of catalyst granules projection image profile minimum, any one this sieve mesh can make by screen cloth and not the catalyst particle by screen cloth be separated.That is, if the minimum parallel tangent distance greater than sieve mesh, this catalyst granules can not pass through sieve mesh, simultaneously the minimum parallel tangent distance will be by sieve mesh less than the catalyst granules of sieve mesh, thereby with separated.Among the present invention, this screening principle is used to remove the catalyst that breaks in addition.Now, screening is described particularly.

Among the present invention, in having the cylindrical or cylinder catalyst of outer diameter A greater than axial length B, as mentioned above, easier the breaking of cylindrical or columnar flat surfaces.As shown in Figure 3, the break minimum parallel tangent distance S of projection image's profile of catalyst is littler than the minimum parallel tangent distance (outer diameter A) of projection image's profile of the normal catalytic agent before breaking.And needless to say, the break minimum parallel tangent distance of projection image's profile of part 3 becomes less than the minimum parallel tangent distance (outer diameter A) of projection image's profile of normal catalytic agent.Here, the minimum parallel tangent distance S that can obtain the above-mentioned catalyst that breaks is as the distance between the tangent line of the tangent line of outermost ledge in the bursting surface of projection image's profile and non-bursting surface periphery, and this tangent line is parallel to the tangent line of ledge.Thus, the catalyst minimum parallel tangent distance S that breaks in the above-mentioned flat surfaces is less than outer diameter A.Therefore, as shown in Figure 5, can use to have rectangle sieve mesh and the width C A that satisfies condition C B and the length L screen cloth that is at least width screens this catalyst, thereby can remove the catalyst that breaks effectively.

In this case, if C greater than A, the non-normal catalytic agent of breaking will be by screen cloth, this is undesirable.In addition, if C less than B, tends to be difficult to remove to have the catalyst that flat surfaces breaks, this is undesirable.Preferred adjusting C has the value of approaching as far as possible value A, thereby can screen the catalyst that breaks effectively until the S that has near A, thereby easily removes the catalyst that breaks.C is preferably with at least 90% of A, preferred at least 95% the as close as possible A of degree.Use therein in the situation according to the commercially available screen cloth of JIS standard (JIS Z8801 1994), disclosed in the JIS normal test sieve standard scale as described, C is the reference dimension of the most close A, and preferably the margin of error in the reference dimension is added to the value that obtains on the C less than value A.Can or allow catalyst flow to screen cloth with a direction (what comprise is reciprocal) by the vibration screen cloth screens.Have length L in utilization and flow with a direction in the situation of screening by making catalyst greater than the screen cloth of the sieve mesh of width C, the direction of preferably regulating L is identical with flowing to of catalyst.In addition, when sieve mesh was rectangle, it can be a slit, as long as length L is more than the width C.Yet along with L is elongated, intensity may reduce.Therefore, preferred L is C≤L≤2C.Consider this point, more preferably square sieve mesh.This for will describe hereinafter to have all screen clothes of rectangular mesh screen purpose be identical.

In addition, have in the situation of screen cloth of circular sieve mesh in use, for outer diameter A than axial length B

Doubly big cylindrical or cylinder catalyst preferably uses the circular sieve mesh diameter C A that satisfies condition〉C〉screen cloth of B, thus can remove the catalyst that breaks effectively.In this case, if C greatly to more than the A, non-normal catalytic agent of breaking will be by screen cloth, this is undesirable.In addition, if C is little to B, becoming is difficult to remove the catalyst that breaks in cylindrical or cylindrical shape flat surfaces, and this is undesirable.The as close as possible A of preferred adjusting C, thus remove the catalyst that breaks easily.

In addition, be under the situation of 1 to 0.5 times cylindrical or cylinder catalyst of axial length B in outer diameter A, cylindrical or columnar tabular surface or break easily as the side of peripheral part.Therefore, in this case, the preferred use has the width C A that satisfies condition〉C〉0.5B and length is at least the screen cloth of the sieve mesh of width, thereby can removes the catalyst that breaks effectively.

In this case, if C greatly to more than the A, non-normal catalytic agent of breaking will be by screen cloth, this is undesirable.In addition, if C is little to 0.5B, tend to be difficult to remove at the cylindrical or columnar catalyst that breaks as the peripheral part side, this is undesirable.In addition, in this case, preferably regulate C and have as far as possible value, thereby easily remove the catalyst that breaks near the A value.

In addition, under the situation of spheric catalyst with outer diameter D, the projection diameter of a circle of rear catalyst of breaking is substantially equal to the projection diameter of a circle of normal catalytic agent before breaking under many circumstances, thereby is difficult to remove the catalyst that breaks with the screen cloth with circle or square sieve mesh.In this case, the preferred use has the width E D that satisfies condition〉E〉0.5D and length L be greater than the screen cloth of the sieve mesh of D, thus can remove the catalyst that breaks effectively.

In this case, if E greatly to more than the D, non-normal catalytic agent of breaking will be by screen cloth, this is undesirable.In addition, if E is little to 0.5D, tend to be difficult to remove the catalyst that breaks, this is undesirable.

Above, described screening technique, wherein used screen cloth with rectangle or circular sieve mesh with reference to the preferred embodiments of the disclosure.Under screen cloth situation, can use rhombus wherein or hexagon sieve mesh inscribed circle diameter screen cloth as C with rhombus or hexagon sieve mesh.If with the shape catalyst of choosing shuttles of the mesh screen with rhombus or hexagon sieve mesh,, will produce fragment and the inexpungible fragment that to remove according to failure mode.Therefore, with respect to spheric catalyst, suggestion avoids using the screen cloth with rhombus or hexagon sieve mesh.

By method of the present invention, can remove the catalyst that breaks with screen cloth, can also remove the catalyst of pulverizing simultaneously.In addition, by changing mesh screen width or diameter ratio, can according to circumstances require to regulate the size of catalyst upper limit of breaking that to remove with screen cloth with respect to the catalyst external diameter.By screening will be only the cracked catalyst of part carry out separating for how much and be difficult to.Yet this catalyst does not influence the reaction tube pressure loss basically, and can handle with the method identical with the normal catalytic agent basically, and therefore, this catalyst is an acceptable in the present invention's screening.

Embodiment

Embodiment 1

In 3.75 parts of pure water, disperse 3.65 parts of basic nickel carbonate (NiCO ₃-2Ni (OH) ₂-4H ₂O).(Carplex#67 is by Shionogi ﹠amp to wherein adding 1.22 parts of silica; Co, Ltd produces) and 2.4 parts of antimony trioxides and abundant the stirring.Heat this slurry, concentrate and dry, and the solid that obtains 800 ℃ of calcination 3 hours.Pulverize calcined product to maximum 60 orders.3.8 parts of pure water to 80 of heating ℃ in the melting pot of agitator is housed, and stir successively and add 1.0 parts of ammonium paramolybdates, 0.135 part of ammonium metavanadate, 0.130 part of ammonium paratungstate and 0.08 part of copper sulphate, and whole powder of obtaining as mentioned above of amount.Heat this slurry that comprises catalytic component and dry to obtain catalyst fines.Then, become with molded this catalyst fines of rotary pelleting machine have external diameter 6mm, the shape of internal diameter 3mm and axial length (highly) 4mm.Calcination is handled the moulded product that obtains 5 hours to obtain catalyst under 400 ℃ of nitrogen atmospheres that comprise 1% oxygen.

Choose with mesh screen and to state catalyst, be recovered in catalyst residual on the screen cloth with 5.6 * 5.6mm square sieve mesh.At that time, the catalyst that reclaims under screen cloth mainly is the catalyst that flat surfaces breaks, and its ratio is to screen 9.5% of catalyst.Then, the alumina balls that mix diameter 4.5mm in the catalyst after screening make mixture be respectively 50% (volume) catalyst/50% (volume) alumina balls (first diluent zone) and 80% (volume) catalyst/20% (volume) alumina balls (second diluent zone) as diluted material.

Above-mentioned second diluent zone of filling loads first diluent zone to 1m then to 1.5m in the stainless steel reaction pipe of internal diameter 27mm and length 5m.

The pipe that pressure gauge and stop valve are housed is connected to reactor head, and is in the stop valve closing state, air is delivered in the pipe, make pressure be calculated as 29.4kPa, open stop valve then and allow air to flow into, read manometric value this moment according to 0 ℃.The pressure evaluation is calculated as 4.5kPa according to 0 ℃ at that time.

Embodiment 2

Prepare catalyst and be seated in the reaction tube according to method identical among the embodiment 1, except the screen cloth with the circular sieve mesh with diameter 5.8mm screens, when read manometric value with the same manner and when allowing air to flow under the same conditions.At that time, the catalyst ratio that reclaims under screen cloth is 9.5% of the catalyst that screens, is 4.5kPa according to the readout at 0 ℃ of calculating pressure meter.

The comparative example 1

Prepare catalyst and be seated in the reaction tube according to method identical among the embodiment 1, except not screening,, read manometric value when with the same manner and when allowing air to flow under the same conditions.The pressure evaluation is calculated as 7.0kPa according to 0 ℃ at that time.

Embodiment 3

Prepare catalyst and be seated in the reaction tube according to method identical among the embodiment 1, except carry out molded make catalyst be shaped as external diameter 6mm, internal diameter 3mm, the height 10mm, and screen with the rectangular mesh screen purpose screen cloth with 5.6mm * 11.2mm, when allowing air to flow in the same manner and under the same conditions, read manometric value.At that time, the catalyst ratio that reclaims under screen cloth is 11.1% of the catalyst that screens, is 3.3kPa according to the readout at 0 ℃ of calculating pressure meter.

The comparative example 2

Prepare catalyst and be seated in the reaction tube according to method identical among the embodiment 3, except not screening,, read manometric value when with the same manner and when allowing air to flow under the same conditions.The pressure evaluation is calculated as 5.8kPa according to 0 ℃ at that time.

Embodiment 4

Prepare catalyst and be seated in the reaction tube according to method identical among the embodiment 1; except using rotary granulator to carry out the molded sphere that is shaped as diameter 6mm that makes catalyst; and screen with the rectangular mesh screen purpose screen cloth with 5.6mm * 11.2mm, when allowing air to flow in the same manner and under the same conditions, read manometric value.At that time, the catalyst ratio that reclaims under screen cloth is 5.6% of the catalyst that screens, is 4.6kPa according to the readout at 0 ℃ of calculating pressure meter.

The comparative example 3

Prepare catalyst and be seated in the reaction tube according to method identical among the embodiment 4,, when allowing air to flow in the same manner and under the same conditions, read manometric value except not screening.The pressure evaluation is calculated as 5.5kPa according to 0 ℃ at that time.

Industrial applicibility

According to the present invention, in reaction tube, before the filling solid catalyst, remove the catalyst that breaks by screening, Thereby can reduce the pressure loss in the reaction tube. Therefore, can under the predetermined running state, react, And the present invention is applicable to filling many kinds of solids catalyst.

Claims

1. the method for a filling solid catalyst, it is characterized by in reactor before the filling solid catalyst, the screening solid catalyst is to remove the catalyst that breaks, wherein have the screen cloth of width as the sieve mesh of C by using, outer diameter A is screened greater than the cylindrical of axial length B or cylindrical solids catalyst, the sieve mesh A that satisfies condition〉C〉B, and the length of sieve mesh is at least width.

2. the method for a filling solid catalyst is characterized by in reactor before the filling solid catalyst, and the screening solid catalyst wherein has the screen cloth of diameter as the circular sieve mesh of C by using to remove the catalyst that breaks, to outer diameter A than axial length B Doubly big cylindrical or cylindrical solids catalyst screens, the sieve mesh A that satisfies condition〉C〉B.

3. according to the method for the filling solid catalyst of claim 1 or 2, wherein the ratio of C and A is at least 90%.